Treatment of carbonaceous and other materials



July 17, 1.928.

F. FRANK TREATMENT OF CARBONACEOUS AND OTHER MATERIALS Original Filed De. 1 1920 2- Sheets-Sheet INVENTOR Ill,

'l IH I IN i ATTORNEYS.

July 17, 1928.

1,677,758 F. FRANK TREATMENT OF CARBONACEOUS AND OTHER MATERIALS Origina iled Dec. 1 .1920 2 Shq 't's-Shebt 2 m l I N I I M t:

l l 1 P I Q 5 Il Q m & I X. 31

,a y L ATTORNEYS.

Patented July 17,1928;

UNITED STATES 1,677,758 PATENT OFFICE.

FELIX FRANK, OF SAN FRANCISCO, CALIFORNIA, ASSIGNOR, BY MESNE ASSIGNMENTS,

TO WILLIAM WALLACE KEMP, F BALTIMORE, MARYLAND.

TREATMENT OF CARBONACEOUS AND OTHER MATERIALS.

Original application filed December 1, 1920, Serial No. 427,566. Divided and this application filed 'J'anuary 2, 1923.

The present invention is a division of my application, Serial No. 427,566 filed December 1, 1920, and has for 1ts prlnclpal ob ect to provide certain new and useful improve- 5 ments in the treatment of materials among which may be mentioned carbonaceous materials, w1th a view, first, to manufacture coke from coal and utilizing and recovermg all by-products; second, to carry'on a dry destructive distillation of peat, lignite,'shale,-

browncoal, coal in general, materials of vegetable origin or structure such as sawdust, wood, roots, leaves and the like, third, to produce water gas, producer gas and the like by completely gasifylng the carbon content in coke or coal and particularly that content in the carbonized residues obtalned in carrying out the process fourth, to manufacture gas for illuminatlng and heating purposes from mineral 011s like crude petroleum; fifth, to manufacture lighter hydrocarbons from' high-boiling asphaltlc residues incident in the refining of petroleum without or with high temperatures or pressures.

Another object is to provide a continuous treatment of the particular material and to utilize a portion of the resultant fuel gas for carrying on the process, at the same tlrne permitting the treatment of large quantlties of the material in a comparatively short time thus rendering the process exceedingly economical both as to the cost of labor and fuel.

One of the principal objects of my invention is the use not only of the recognized physico-chemical properties of a flame, such as size, shape, colorific intensity, heat concentration and flame propagation, butalso to subject the material to be treated to molecular or ionical wave movement, vibration or bombardment taking place or originating in the flame zone. It is my theory that the molecules and ions of the burning substances which form the flame revolve and circulate with such enormously high velocity that when the material to be treated is interposed as an obstacle in their path it is subjected to and undergoes a violent bombardment of molecules and ions and the attendant severe friction between the molecules and ions of the flame components and those of the maierial to be treated probably imparts certain Serial No. 610,290.

vibrations to the latter which serve to accelerate the 'chemical reactions to be achieved by the process. I also maintain that there are molecules and ions of the flame components which move about within the flame or radiate therefrom in form of innumerable waves the length of which lies between and beyond that of the infra-red and the ultra-violet. I believe that when the material -to be treated is placed in the path of these waves it acts as a breaker and that it is penetrated partly or wholly by these waves and a. molecular or ionical movementor vibration is thereupon set up within the material to be treated which facilitates, accelerates or makes possible the desired reactions.

As the material to be treated is being sub jected tothe direct action of the flame which may be luminous or non-luminous, visible or invisible. the material in or near the flame is probably first raised to approximately flame temperature at which temperature the material may be incandescent or glowing. Then the next nearest strata or layer of material is being raised to the temperature of the flame and I have observed that the flame zone is being widened, deepened or enlarged in the measure as the Volume of material is heated to approximately flame temperature. When the material to be treated has been heated to a high temperature the combustible mixture of materials including oxygen which issues from the burner on which the flame originally is produced will in whole or in part not only burn on the'burner orifice but Wlll also burn within the voids throughout the entire mass of the material under 4 treatment. This may be partly explained by the enormous expansion in the volume of the combustible mixture of materials including oxygen on issuing from the burner orifice onto the material to be treated. The increase in volume brings about an increase in the velocity of the combustible mixture of materials including oxygen which is then driven or forced into the voids of, in and between the material tobe treated until its velocity has again reached a point where the rate of flame propagation is about equal to the velocity of the combustible mixture of materials including oxygen and the combustible mixture will then burn at about the ture and to attain this object they arebrought into direct intimate contact with the live flame itself.

In order to produce the desired result, use is made of a process which consists essentially in subjecting the material, under the exclusion of atmospheric air, to the direct action of a flame preferably produced by burning a previously formed combustible mixture of fuel gas and air in a predetermined ratio to heat and in case a reducing flame is employed as shown and described in my co-pending application, Serial No.

427,566, filed Dec. 1, 1920, reduce the material without igniting or burning the same.

To treat the different materials above referred to by the process mentioned use has necessarily to be made of different apparatus such, for instance, as shown in the accompanying drawings, in which similar characters of reference indicate correspondin% parts in all the views.

gure 1 is a side elevation, with parts in section, of one form of apparatus for carrying out the treatment;

Figure 2 is an enlarged longitudinal central section of the retort of the apparatus shown in Figure 1.

Figure 3 is a longitudinal section through a catalytic converter box.

In the apparatus shown use is made of a revoluble cylindrical retort 10, slightly inclined and having heads 11 and 12 resting on wheels 13 and 14 journaled in bearings 15 and. 16 mounted on suitable foundations 17 and 18. At least, one of the wheels 14 is connected by a gearing 19 with a motor 20 of any approved construction to rotate the retort 10 at a comparatively slow speed, according to the nature of the material to be treated.

The material to be treated may be delivered by a conveyor screw 25 into the upper "end of the retort 10, and this conveyor screw is preferably secured to a hollow shaft 26 extending cent-rally into the retort, and being secured to brackets 27 attached to the retort to cause the shaft 26 and the conveyor screw 25 to rotate with the retort.

The conveyor screw 25 turns in a cylindrical casing 28 extending through a stuffing box 29 attached to the upper retort head 12.

The material to be treated is contained in a hopper or bin 30 having an outlet 31 opening into the conveyer casing 28 and in this outlet 31 is arranged a measuring wheel 32 rotated at a predetermined speed to feed the material in predetermined quantities into the casing 28 to be carried by the conveyer screw 25 into the upper end of the retort 10. The measuring wheel 32 is mounted on a shaft 33 carrying a pulley 34 connected with other machinery for imparting the desired rotary motion to the measuring wheel 32. The hollow shaft 26 of the conveyer screw 25- forms an exhaust pipe for carrying off the volatile matter from the retort 10 and for this purpose the shaft 26 is provided with apertures 35 opening into the retort.

The outer end of the hollow shaft 26 is journaled in a stuffing box 36 arranged on the head 37 closing the outer end of the conveyer casing 28. A suction pipe 38 con-' 'nects with the stuffing box 36 and forms a continuation of the exhaust pipe formed by the shaft 26, and this suction pipe 38 connects with an exhaust fan 40 of any approved construction to draw the volatile Method of producing the flame.

In as much as the flame is produced by burning a previously formed combustible mixture of material including oxygen or any other supporter of combustion within an air-tight container it is desirable to feed the combustible mixture to the burner at a velocity higher than the rate of flame propagation corresponding to the mixture at the temperature prevailing within the air-. tight chamber and also to take into consideration the pressure or vacuum prevailing within said chamber which will otherwise reduce or increase the volume of combustibles discharged from the burner orifice. If the velocity at the burner is too low the combustible mixture will back fire and explode; if it is too high the flame cannot be held or maintained at the burner. At the right velocity the combustible mixture will burn on the burner.

Within the lower portion of the retort 10 is arranged a burner 50 for burning a previously formed combustible mixture of fuel gas and air in a predetermined ratio thereby producing a flame projected downwardly onto the material as the latter is moved forward within the inclined retort 10 during IOU the rotary motion thereof. The heat emanating from the flame besides heating the material causes a heating of the retort 10, which latter is preferably provided with a lining 51 of fire brick or other refractory material to readily withstand the heat. The burner 50 is mounted on the inner end of a supply pipe'52 extending through the lower end of the retort and provided at its outer portion with a valve 53 to control the amount of combustible mixture of fuel gas and air burned at the burner 50. The supply pipe 52 is connected with a mixing device 54 of any approved construction, and this mixing device 54 is connected with a gas supply pipe 55 having a valve 56 and extending into a gasometer 57 of usual construction. The mixing device 54 is used for mixing the fuel gas from the gasometer 57 with air in a predetermined ratio to produce at the burner either a neutral flame, an oxidizing flame, or a reducing flame, as hereinafter more fully explained. The mixing device 54: may be of any suitable type adapted to provide a mixture of the character required. An example of such a device is disclosed in the U. S. patent to Kemp and Van Horn No. 1,420,658, dated June 27, 1922.

A neutral flame is produced within the air tight retort 10 when the amount of fuel gas and air is in the proper proportion to produce complete combustion. If an excess of air is in the mixture then an oxidizing flame is produced owing to the atmospheric oxygen content in the surplus of air not being consumed. If a less amount of air than that required for a neutral flame is mixed with the gas then a reducing flame is had, which contains an excess of hydrogen. It is understood that the mixing device 54*. is adjusted to produce the desired mixture of fuel gas and air in the proper ratio for producing the desired flame above mentioned.

Neutral flame.

temperature. It will be noticed that in view of the absence of atmospheric air within the retort 10. kept under a slight vacuum, the

neutral flame fulfills'two missions in that it first heats the material in the retort 10 at the desired temperature and at the same time subjects it to the influence of the superheated steam contained in the products of combustion. The other elements present in the products of combustion, like nitrogen, are. for all practical purposes inert, it being understood that the sulphur in the original fuel gas has been removed by the usual purification methods. Thus it is evident that a neutral flame as described cannot ignite or burn even an inflammable material as no free oxygen is present which could maintain such a combustion.

Reducing flame.

in the retort to the desired temperature,

second, to subject the material to the influence of superheated steam contained in the products of combustion; and third, to subject it to the influence of free superheated hydrogen contained in the products of combustion of such a reducing flame and, under certain conditions, also to the influence of free carbon monoxide contained in the products of combustion. In regard to the possibility of free oxygen being present in the reducing flame, it may be stated that the hydro-carbons have a much greater aflinity for oxygen at high temperature flames as compared with either that of hydrogen or carbon monoxide. Thus in the explosion of a mixture corresponding to C H +H +O there is practically no formation of steam. This is especially true under the conditions under which this reducing flame burns inside of the retort for the absence of free or atmospheric oxygen within the retort due to the action of the exhaust fan, prevents even the partial oxidation of this free hydrogen through secondary air or oxygen on the outer flame film or cone. It is expressly understood that the only oxygen admitted to the retort is that which has been premixed with'the fuel gas in the form of air before t reaches the burner within the retort. In order to produce a reducing flame this admitted oxygen is insufiicie nt for complete combustion of the hydrogen and as the" retort is devoid of oxygen the hydrogen cannot possibly become oxidized. The presence of free hydrogen especially at high temperatures in such reducing flames makes it possible to obtain valuable results in the hydrogenation of certain oils but it is of great importance particularly in the distillation and refining of crude mineral oils and asphalts in the retort as the various fractions obtained by means of the process described and those. salts of phos-- phorus, being rich in oxygen, which are used as catalysts, are in many cases more valuable and the yield much higher than those obtained by the usual methods of distillation. Especially in the distillation of crude paraflin base oils does my method increase the yield of valuable lubricating oils at the expense of the less valuable red parafiin mass. In the distillation of asphaltum base oils increased yields of high-boiling and viscous oils are obtained at the expense of the almost valueless pitch residue orditil ' with the original mixture of fuel gas andair,

lit)

narily remaining in the common refinery still.

Oxidising flame.

The oxidizing flame burning in the retort also fulfills three missions: First, to heat the material in the retort to the desired temperature; second, to subject the material to the influence of superheated steam contained in the products of combustion; and, third, to subject the material to the influence of free superheated oxygen and under certain conditions to the influence of free carbon monoxide; for instance, if a mixture of 1 art by volume of water gas (composed of equal parts by volume of h dlogen and carbon monoxide), 2.41 parts by volume'of atmospheric air, and 1- part by volume of oxygen, are burned in the retort under conditions already fully described, then a quantity of oxygen equal to the 1 part of oxygen mixed will be contained or mingled or mixed With the products of combustion in a free, but enormously superheated state of approximately the flame temperature, and'will be available for action, in presence or in the ab sence of catalysts, like copper, iron, nickel, tungsten, vanadium, platinum, etc., their oxides and salts, upon the material in the retort to be subjected to such oxidizing action. On account of the ease with which oxygen at such high temperature can be applied it is now possible with my method to produce oxygen addition products from hydrocarbons, which could not be obtained heretofore except by employing pressures in autoclaves so high, that in practice they could not be used. With my method oxygen at flame temperature of any combustible gas can be obtained Without pressure autoclaves. The most valuable action of the oxidizing flame if used in vthe presence of those salts of phosphorus rich in oxygen and stable at a igh temperature like tricalcium phosphate consists in the fact that during the distillation of asphaltum or paraffin base mineral oils or coal tars or lignitic tars or shale tars, as Well as certain vegetable oils, entirely different fractions and oils of an entirely different chemical composition are obtained and under the distillation of the very same materials at the very same temperatures with the above described reducing flame or with a neutral flame.

\Vhen a predetermined excess volume of hydrogen is mixed with the required mixture of fuel gas and air, then an equal quantity by weight of hydrogen will appear free, in superheated state, among the roduets of combustion, and will be availa le for hydrogenation and the formation of hydrogen addition products.

From the foregoing it will be seen that by the describedprocess and apparatus I can obtain from the same mineral oil or tar three different series of fractions by using either a neutral flame, a reducing flame or an oxidizing flame.

The flame burning in the retort and brought in contact with the material to be treated and containing volatile matter like lignite heats up this material to the maximum flame temperature and thus separates all volatile matter contained in the material and which volatile matter together with the products ofcombustion is carried off through the hollow shaft 26 by the action of the exhaust fan 40, thus leaving a carbonized residue in the retort. The retort is heated by the flame and hence the material dropped by the conveyor screw 25 in the upper end of the retort is subjected to the retort heat and thus gives off its moisture which is carried off with the volatile matter through the hollow shaft 26. The speed of the retort 10 is so adjusted that the flame heatsthe materialto over 100 C. when passing under the flame. In case lignite is treated, for instance, at about 250 C. the superheated'water vapor contained in the products of combustion interacts with the volatile matter of the lignite to form Montan Wax, carried through the hollow shaft 26, to be subsequently condensed as hereinafter more fully explained. Under certain conditions the pipe 38 (after leaving the retort and as illustrated in F igure 3) enters a catalytic converter box A containing a number of electrically heated copper, platinum, iron, nickel, etc., wires, and which has a number of air inlets B. These air inlets B can be opened and closed by means of valves not shown on the drawing. The condensable and non-condensable gases generated in the retort enter the converter box, where they come in contact with the oxygen contained in the atmospheric air sucked in through the air inlets B in presence of the red hot catalytic agents, like iron, copper, nickel, vanadium, thorium, etc. wires and, under certain conditions become further oxidized.

The above is of great importance, for instance, when wood or saw dust is being subjected to destructive disillation within the retort, as already described, and it is desired to convert all or part of the produced wood alcohol vapors into formaldehyde. In that case theconverter box A is provided with electrically heated copper wires which will bring about the interaction between the oxygen contained in the atmospheric air admitted through the air inletsv the desired temperature it will not be necessary to heat the catalysts in the converter box. They can in fact be present in the converter in form of lumps, powder, granules, asbestos sponge impregnated with a salt or oxide of these catalysts, or in any other convenient form.

There are given off in the course "of the forward travel of the lignite considerable volumes of burnable, non-condensable gases, and a certain quantity of ammonia vapors, all of which are exhausted from the retort by way of the hollow shaft 26. Dust or other solid matter liable to arise during the forward movement of the material in the retort 10 is carried off with the vapors and gas to settle in the chamber 42, as reviously mentioned. The quantity of yield .of Montan wax is greatly improved by the use of catalysts'such as salts of phosphorus which are rich in oxygen and stable at high temperatures, for instance, tricalcium phosphate. The catalysts can be mixed either with the lignite or they can be embedded in the lining 51 of the retort in thevicinity of the hottest zone. The use of the catalysts results in the production of a crude Montan wax better in purity and color than that obtained without such catalysts, and it is refined easier with a larger yield of ceresin and montanic acid. The residue of coke, on

reaching the lower end of the retort 10 is lifted by lifting arms attached to the inner surface of the lining 51, and the lifted residue is finally dropped into the inner end of the conveyer casing 61 extending through a stufling box 62 arranged on the head 11 of the retort 10. The inner end of the conveyor casing 61 is provided on top with a cut-out portion 63 to allow the lifted residue to drop into the casing to be moved along the same by a conveyor screw 64 secured to a hollow shaft 65 through whlch extends the supply pipe 52 of the burner 50. The inner end of the hollow shaft 65 is secured to a bracket 66 carried by the retort 10 and the other end of the said shaft is journaled in a stufling box 67 attached to the head 68 closing the outer end of the conveyer casing 61. It will be noticed that when the retort 10'is revolving a rotary motlon is given to the conveyer screw 64 to move the residue along the casing 61 into an outlet 70 extending with its lower end into water 1 contained in a tank 72. The outlet 70 3S provided with a discharge wheel 73 attached acid) water supplied from a suitable source by a valved supply pipe 82. The pipe 80 extends within a short distance of the bottom of this vessel 81 and the lower end of this vessel connects with a siphon 83 for drawing'off the liquid in the vessel 81 and maintaining the liquid at a predetermined level therein. The siphon 83 is provided at its discharge end with a suitable valve 84. The upper end of the vessel 81 connects by a pipe 85 with another closed vessel 86, preferably made of iron, and containing a caustic soda solution. The pipe 85 extends within a short distance of the bottom of this tank 86, as shown in Figure 1. The upper end of the vessel-86 connects by a suction pipe 90 with a suction fan 91 having its discharge pipe 92 provided with a valve 93 discharging into the gasometer 57. A pipe 91 leads from the gasometer 57 for drawing olf surplus gas for other purposes. The pipe 94 is provided with a suitable valve 95. 'By the use of suitable chemical solutions in the vessels 81 and 86 the condensable gases are condensed, and the non-condensable fuel gas is drawn off by the suction fan 91 and discharged into the gasometer 57, thus providing a supply of fuel gas for use in the mixing device 54 to form the combustible mixture burned at the burner 50. The mixture at the burner 50 is ignited by a suitable spark plug or other means. In case of treating lignite in the apparatus, a weak sulphuric acid solution in the vessel 81 acts as a condenser for the Montan wax, and absorbs the ammonia vapors present in the gases. The caustic soda solution in the vessel 86 absorbs the greater part of the carbon dioxide contained in the products of com- .bustion incident to the burning of the flame at the burner 50 and carried along with the gases. In case analysis shows the nitrogen contents of the gas in the gasometer 57 to be too high, then the gasometer is supplied with fresh city gas, or the greater part of the gas in the gasometer 57 is allowed to escape and then the full strength gas used as it comes from the suction fan 91. In treating other materials the settling tank 42 may be dispensed with and in this case the gas is directly delivered to the vessel 81 by extending the pipe 38 into as the pipe 80.

the vessel the same Manufacture of coal tar from bz'twm'nous I coal. In the manufacture of coal tar from bituminous coal the same general method as that described in the manufacture of Montan wax is employed, except that the temperature may be higher, if high temperature tars are desired, or lower, if low temperature tars (Urteer or Tiefteer) are desired. Instead of -Montan wax-ordinary coal tar,

however, is obtained in the vessel 81. The crude coal tar, however, is re-distilled in the same manner as crude mineral oils.

Distillation anal refining of distillable min eral oil including coal tars, shale and Zigmitic tars, aspkaltum and coal tar pitch.

When using the rotary retort 10 the hopper 30 is dispensed with and the liquid oils or tars, heated if necessary, are allowed to flow into the upper end of the retort 10 in a measured steady stream. The flame emanating from the burner 50 is so adjusted that all the desired Volatile matters are given off before the residue arrives at the lifting members 60 which deliver it to the Conveyor screw 64. If the residue is a liquid the lifters 60 are of spoon or bowl shape. In case there is a tendency to carbonize on the walls of the retort 10 in the hot zone a number of pebbles or iron balls are used in the retort and allowed to roll in it for the purpose of knocking off an matter that may adhere to the retort wa ls. As stated before, the crude tars. referred to can be made to yield different fractions or distillates by using either a neutral flame, an oxidizing flame or a reducing flame in the presence of catalysts in the form of salts of phosphorus, calcium or nickel rich in oxy gen or in the form of already formed residue or coke and ash. It will also be noticed that the very presence of minute quantities of such catalysts improves the color and purity of the distilled oils or waxes and increases the yield. These results are especially noticeable in the distillation of paraffin oils or paraffin base tars.

In the manufacture of fuel gas from coal or coke steam is introduced in the same manner as described. The improvements described afiord a means for the utilization of coke or coal dust without briquetting.

By subjecting lignite or coal to the direct action of a flame produced by burning a combustible mixture of fuel gas and air in a predetermined ratio, under exclusion of atmospheric air, within an airtight kiln or retort, from which the volatile matters are removed by means of a suction fan, I obtain coke as residue, provided-that I do not heat this oke higher than that temperature at which the highest boiling fraction of the volatile matters distills over: or in other words, provided that the coke is not subjected to a flame temperature which lies materially higher than the highest boiling point of the last fraction.

In'order to utilize this coke, whether in form of large lumps, breeze or dust, it is ntroduced in a measured, steady volume into the kiln 10, the inside of which is kept at a temperature of from 600 centigrade to 1600 centigrade. Into this kiln is also introduced, together with the coke, a measured, steady volume of superheated steam. In order to hasten and intensify the reaction I use as catalysts either ,iron, copper, nickel, tungsten, vanadium, their oxides,

peroxides or other salts. Between 600 and 1600 centigrade the carbon contained in the coke in the presence of catalysts'will cause the hydrogen and oxygen contained in the steam to disassociate, whereupon the freed oxygen will combine with the carbon, for

which it has a larger affinity, causing the for 'mation of carbon monoxide, which together with the free hydro en is removed from the volatile matter and all fixed carbon in lignite and coke at the same time inthe same operation. In that case the volume of gases will be enlarged by that portion produced through the gasifica'tion of the volatile hydro-carbons, and the resulting gas will not be simply a mixture of hydrogen and carbon monoxide, as above, but will also contain a certain percentage of methane and the like.

The introduction of steam into the kiln, in the'presence of the above named cata lysts, is also important in the distillation of shale oil, mineral oils and Wood.

In the manufacture of acetic acid, pyroligneous liquor and the like from sawdust wood and similar material, the same genera method of distillation is employed as above described for the manufacture of Montan wax exce t that the vessel 81 contains only water an the vessel 86 contains an oxide of lime solution.

Shales, browncoal, peat and similar materials are distilled in the same manner as H described relative to the manufacture of Montan wax. A

-, An important advantage of the processdescribed is the ease with which heavy hydrocarbons, especially pitch residues, can be cracked with the accompanying yield of mobile,lighter oils and lubricating oils. If the same method is used on ordinary crude mineral oil as it comes from the well an increased yield of all fractions is obtained at the expense of carbon residues remaining usually in the refinery stills when the ordinary still methods are employed. If, for

instance, it is desired to crack Mexican fuel then sprayed into the retort under a pressure of 50 lbs. The oil globules are heated to the desired temperature as they pass through the flame zones and the residue, whether pitch or carbon, is drawn off. The process described can be used for all temperatures and pressures but the mixture of gas and air to be burned at the burner must always be under a pressure higher than that of the incoming oil or other spray.

For the drying of wet organic and inorganic materials the water vapors can be condensed or they may be blown intothe' air by an exhaust fan. In this case the solid crystals settle after the liquid globules have been evaporated to dryness during their passage through the flame zones. As the flames do not contain any soot or other discolor'ing material and burn, in fact, with an almost in-- visible blue flame, the material cannot be discolored. A For the manufacture of carbon dioxide as a by-product from the production of burned lime or cement clinkel' from clay and lime stones enough of the gas and air mixture is burned at the burner 50 to produce a Very hot torch flame the same as is ordinarily employed in cement kilns. The carbon dioxide, together with the products of combustion are removed by the exhaust fan 40 and are delivered direct to an absorption tower or compressing apparatus for liquefaction. that the expression under exclusion of atmospheric air used in the specification means that an air tight retort or chamber is used in which the material is subjected It should be here mentioned:

to the flame. In other words, the material is subjected to the flame Within a chamber or retort from which air or other substance capable of supporting combustion is excluded.

I claim: I

1. The herein described process for the treatment of heat dissociable materials which consists in introducing the material into an air-tight chamber and subjecting the same to the direct action of a flame produced by burning a previously formed mixture of uniform composition, containing as constituents combustible material and a supporter of combustion, including an excess of a reducing agent, thereby heating the material to dissociate the same into volatile matter and residue and carrying out a chemical reaction by the action of an element of the reducing agent on an element of the material being treated.

2. The herein described process for the treatment of heat dissociable materials which consists in introducing the material into an air-tight chamber and subjecting the same to thedirect action of a flame produced by burning a previously formed mixture of uniform composition, containing as constituents combustible material and a supporter of combustion, including an excess of hydrogen, thereby heating the material to dissociate the same into volatile matter and residue and carrying out a chemical reaction by the action of the hydrogen on an element ofthe material being treated.

' FELIX FRANK. 

